CN102634363A - Three-tower type atmospheric-vacuum tar distillation process - Google Patents
Three-tower type atmospheric-vacuum tar distillation process Download PDFInfo
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Abstract
The invention relates to a three-tower type atmospheric-vacuum tar distillation process. A raw material tar is dehydrated to obtain light oil fractions under constant pressure in a pre-dehydrating tower and a dehydrating tower, carrying out constant pressure operation in a No. 1 distillation tower to obtain carbolic oil and naphthalene oil fractions, and carrying out reduced pressure operation in a No. 2 distillation tower to obtain washing oil, primary anthracene oil, secondary anthracene oil and medium-temperature asphalt under or obtain the washing oil, the primary anthracene oil and maltha products. Heats of the pre-dehydrating tower and the dehydrating tower are provided by heat-conduction oil or steam; the heat of the No. 1 distillation tower is circularly provided by tower bottom mixing oil in a No. 1 tube-type heating furnace; and the heat of the No. 2 distillation tower is circularly provided by tower bottom asphalt in a No. 2 tube-type heating furnace. A main device comprises the dehydrating tower, the No. 1 distillation tower, the No. 2 distillation tower, a dehydrating tower reboiler, the No. 1 tube-type heating furnace, the No. 2 tube-type heating furnace, each fraction heat exchanger, a cooler, a pump and the like. The three-tower type atmospheric-vacuum tar distillation process disclosed by the invention has the advantages of being simple and quick in process flow, simple and convenient in operation, low in capital construction investment, energy-saving and environment-friendly, and is suitable for coal tar processing engineering capable of annularly processing anhydrous tar in the scale of more than 2,000,000 tons.
Description
Technical field
The present invention relates to metallurgical coking industry coal tar processing technical field, is a kind ofly through the distillatory method tar separation to be obtained the technology and the equipment thereof of various fractions and viscid bitumen or mid-temperature pitch, is specially adapted to big-and-middle-sized coal tar process engineering.
Background technology
The coal tar oil composition is extremely complicated, comprises up to ten thousand kinds of components such as aromatic hydrocarbons and heterogeneous ring compound, and can process the product that obtains has kind more than 200.Wherein heterogeneous ring compound such as aromatic hydrocarbons such as naphthalene, anthracene, phenanthrene and thiophene, indoles, pyridine, quinoline and phenols are distinctive very rare Chemicals in the coal tar.Coal tar processing is made up of roughing out and deep processing two parts; The first step of roughing out is a tar distillation; Tar distillation is the tap of whole coal tar processing thus, and the separating effect of tar distillation directly influences quality product, yield and the energy consumption of follow-up deep processing.At present both at home and abroad enterprise adopt usually, the reliable tar distillation technology of technical comparative maturity has three kinds of air distillation, atmospheric and vacuum distillation and underpressure distillation.
Air distillation technology is that raw tar gets into flash distillation in one section vaporizer in tube furnace convection zone heating back, and water and part light oil are deviate from the top, and the bottom anhydrous tar gets into flash evaporator after sending into the heating of tube furnace radiation section.Mid-temperature pitch is isolated in the flash evaporator bottom, and side line cuts the anthracene oil fraction, and the fraction steam of overflowing in the top gets into the fraction tower.Fraction column overhead extraction light oil fraction, from top to bottom side line cuts carbolic oil, naphtalene oil, washing oil and a carbolineum fraction successively, and carbolic oil, naphtalene oil and washing oil fraction also can be used as three and mix fraction extraction together.In order to improve the yield of high value added products such as phenol, naphthalene, adopt the technical process that cuts three mixed fractions usually.In order to reduce distillation temperature, flash evaporator and fraction tower bottom feed superheated vapour.One section all operation under normal pressure of vaporizer, flash evaporator and fraction tower.
It is the shortest that two kinds of technologies of air distillation technology and other are compared technical process, and initial cost is minimum, good operation, easy to control, but the coal gas consumption is higher.Because the separation of fraction is in same tower, to accomplish, distillation institute heat requirement is provided by a tube furnace, limit by tube furnace device structure designing institute, and single covering device processing power is lower, is 200,000 tons of year processing anhydrous tars to the maximum.When cutting three when mixing fraction, fraction repeats heating in the subsequent production device, strengthened energy consumption.And the open steam that feeds contains phenol, ammonia waste water through becoming after the oily water separation, increased the water pollution.
Atmospheric and vacuum distillation technology is the water of in the dehydration tower of atmospheric operation, deviating from after the raw tar preheating in the tar, and the extraction light oil distillate, and anhydrous tar is sent into pre-distillation column at the bottom of the tower.Pre-distillation column also is an atmospheric tower, and by the tube furnace circulation heating, and extraction asphaltic products., cat head get into quench tower after deviating from the ammoniacal liquor chilling that the bituminous wide fraction sprayed at the bottom of the tower, and after adding alkali and separating, wide fraction gets into separation column.Separation column is under reduced pressure operated, and cat head extraction carbolic oil fraction, side line cut carbolic oil, naphtalene oil, washing oil and a carbolineum fraction from top to bottom successively, extraction anthracene oil fraction at the bottom of the tower, separation column distillation institute heat requirement by tower at the bottom of anthracene oil get into tube furnace circulation heating and provide.
Atmospheric and vacuum distillation technology fraction is cut apart thinner, reduces the heating that repeats of following process fraction.But the heaviest component bituminous separates the employing air distillation in the tar, and underpressure distillation is adopted in other separation than light constituent, and pressure distribution is not too reasonable.And main fraction twice heating in fore-distillation and vacuum fractionation process in the tar, the gas consumption amount is big.This technology is external patented technology, the domestic precedent that introduction was once arranged, because complex process, equipment is various, and initial cost is very big, on-the-spot actually operating difficulty.
Reduced pressure distillation process is divided into single tower and two kinds of two-tower types.
Single tower type pressure reducing distil process is to get into preparatory dehydration tower after the raw tar preheating, and cat head is deviate from most of water and a small amount of light oil, and the tar at the bottom of the tower is from flowing into dehydration tower.Dehydration column overhead distillates residue light oil fraction and water, and anhydrous tar advances that the tube furnace heating is laggard goes into king-tower at the bottom of the tower.Dehydration tower and dehydration tower are atmospheric operation in advance, and king-tower is a decompression operation.King-tower cat head extraction carbolic oil fraction, side line cuts naphtalene oil fraction, washing oil fraction and carbolineum fraction, extraction viscid bitumen at the bottom of the tower.
Single tower type pressure reducing distil process fraction tower is under reduced pressure operated, and has both reduced distillation temperature, has reduced the coking of tube furnace again, also helps environment protection.But because anhydrous tar need separate into a plurality of fractions in single tower, between each fraction cutting meticulous inadequately, cause high value added product to run off easily.Distillation institute heat requirement is to be provided by a tube furnace equally, and single covering device processing power is 200,000 tons of year processing anhydrous tars to the maximum.
The two-tower type pressure reducing distil process in advance the process of dehydration and dehydration with single tower identical, entering 1# distillation tower after anhydrous tar and 1# base product turning oil mix, advance the 1# tubular oven and heats at the bottom of the dehydration Tata.1# distillation tower cat head extraction carbolic oil cut, side line extraction naphtalene oil fraction and fine laundering oil fraction, mixing oil mixes, advances 2# tubular oven heating back entering 2# distillation tower with circulation pitch at the bottom of the 2# distillation Tata at the bottom of the tower.The heavy wash oil fraction of 2# distillation tower cat head extraction, side line extraction one carbolineum fraction and anthracene oil fraction are produced mid-temperature pitch at the bottom of the tower.1# distillation tower and 2# distillation tower are all operated under reduced pressure.
The two-tower type pressure reducing distil process is compared with single tower type pressure reducing distil process, and being separated in two distillation towers of each fraction accomplished, and cut is cut apart thinner, and single covering device processing power is bigger.Two distillation towers all are decompression operations, have effectively reduced service temperature, but two cover vacuum systems have increased operation easier, the corresponding vacuum system of 1# distillation tower particularly, because the existence of naphthalene component, equipment, pipeline are prone to stifled, have hindered the continuous operation of system.
Can find out that from above comparison existing tar distillation technology respectively has characteristics, and its weak point is all arranged.It is short to invent a kind of technical process, and good operation, reduced investment, energy consumption is low, environment protecting good, the novel process that can adapt to the processing of maximization tar is the market demand of domestic and international metallurgical coking industry.
Summary of the invention
The purpose of this invention is to provide the normal vacuum tar distil process of a kind of three-tower type; This process tars dehydration and being separated under the normal pressure of light constituent are carried out; The separation of heavy constituent is under reduced pressure carried out; Technical process is simple and direct, easy and simple to handle, initial cost is supported, energy-conserving and environment-protective, is applicable to the tar processing of year processing anhydrous tar scale more than 200,000 tons.
For realizing above-mentioned purpose, the present invention realizes through following technical proposals:
The normal vacuum tar distil process of three-tower type may further comprise the steps:
1) raw tar is removing moisture and extraction light oil fraction in dehydration tower, the dehydration tower in advance under condition of normal pressure, and the heat of dehydration tower, dehydration tower is provided by thermal oil or steam in advance;
2) dehydrated tar under condition of normal pressure in the 1# distillation tower fractionation by distillation, cat head extraction carbolic oil fraction, side line cuts the naphtalene oil fraction; The heat of 1# distillation tower by tower at the bottom of mixing oil provide in 1# tubular oven internal recycle heating;
3) 1# base product mixing oil in the 2# distillation tower under reduced pressure fractionation by distillation obtain washing oil, a carbolineum, anthracene oil fraction and asphaltic products.; Or washing oil, a carbolineum fraction and viscid bitumen product.The heat of 2# distillation tower by tower at the bottom of pitch provide in 2# tubular oven internal recycle heating.
The normal vacuum tar distil process of three-tower type has dehydration, 1# distillation, the main Distallation systm of 2# distillation three covers.
1. dewatering system
The effect of dewatering system is the moisture that removes in the tar, and this system's major equipment has extractor pump etc. at the bottom of recycle pump at the bottom of preparatory dehydration tower, dehydration tower, the tower, dehydration tower reboiler, the tower, and each equipment passes through pipe connection.
Raw tar finally removes moisture and extraction light oil fraction in dehydration tower after preparatory dehydration tower flash distillation, anhydrous tar returns in the tower so that heat to be provided after delivering to the reboiler heating by recycle pump at the bottom of the tower.The dehydration tower reboiler can be with steam or heat-conducting oil heating.
Dehydration tower is under condition of normal pressure, to operate; Absolute pressure of top of the tower 101～107kPa, 95～120 ℃ of tower top temperatures, 180～210 ℃ of column bottom temperatures; 195～230 ℃ of dehydration tower reboiler circulation tar temperature outs, dehydration column overhead light oil reflux ratio (to anhydrous tar) 0.02～0.04t/t.
Dehydration tower is a tray column, can adopt the novel float valve in wide aperture, also can adopt the various new tower plate that are applicable to the coal tar medium, and material is a stainless steel, and 6～10 blocks of theoretical trays are arranged.
The dehydration tower reboiler is vertical liquid film downward flow type structure, and turning oil flows from top to bottom, and material is a carbon steel.
2.1# Distallation systm
The effect of 1# Distallation systm is carbolic oil and the naphtalene oil cut of isolating in the tar.These two kinds of cuts are components lighter in the raw tar; So the present invention selects this system under condition of normal pressure, to operate, system compares with decompression operation, has reduced a cover vacuum apparatus such as vacuum pump, vacuum cooler-condenser; Reduce one-time investment, also reduced the complicacy of operation.1# Distallation systm major equipment has recycle pump at the bottom of 1# distillation tower, cat head reduction appts., fraction interchanger, water cooler, tubular oven, the tower, cut extraction pump etc., and each equipment passes through pipe connection.
Dehydrated tar is fractionation by distillation in the 1# distillation tower, cat head extraction carbolic oil fraction, and side line cuts the naphtalene oil fraction, and mixing oil gets into the 2# Distallation systm at the bottom of the tower.The heat of 1# distillation tower by tower at the bottom of mixing oil provide in 1# tubular oven internal recycle heating.
1# distillation tower tower top pressure is controlled at absolute pressure 101～107kPa; 160～190 ℃ of tower top temperatures; 210～240 ℃ of naphtalene oil fraction extraction plate temperatures; 265～295 ℃ of column bottom temperatures, 290～320 ℃ of 1# tubular oven turning oil temperature outs, cat head carbolic oil reflux ratio (to anhydrous tar) 0.45～0.7t/t.
The 1# distillation tower is a tray column, can adopt the novel float valve in wide aperture, also can adopt the various new tower plate that are applicable to the coal tar medium, and material is a stainless steel, and 22～32 blocks of theoretical trays are arranged.
The 1# tubular oven is vertical coil pipe cylindrical furnace, and upper of furnace body is energy-conservation section with flue gas heat exchange, and the bottom is a radiation section, and furnace tube material is a stainless steel.
3.2# Distallation systm
The effect of 2# Distallation systm is 1# to be distilled the mixing oil that comes at the bottom of the Tata separate into wash oil fraction, carbolineum cut and asphaltic products..Pitch is component the heaviest in the raw tar, and fractionation by distillation needs higher service temperature under normal pressure, and generally also need feed open steam, produces phenolic wastewater after the oily water separation.So the present invention selects this system under reduced pressure, to operate, distillation tower is operated under lower temperature, and need not be fed open steam.2# Distallation systm major equipment has recycle pump at the bottom of 2# distillation tower, cat head reduction appts., fraction interchanger, water cooler, tubular oven, the tower, cut extraction pump, vacuum pump, vacuum cooler-condenser etc., and each equipment passes through pipe connection.
By mixing oil fractionation by distillation in the 2# distillation tower of coming at the bottom of the 1# distillation Tata, cat head extraction washing oil fraction, when producing the viscid bitumen product at the bottom of the tower, the tower side line only cuts a carbolineum cut; When producing the mid-temperature pitch product at the bottom of the tower, the tower side line cuts a carbolineum cut and anthracene oil cut.The heat of 2# distillation tower by tower at the bottom of pitch provide in 2# tubular oven internal recycle heating.
2# distillation tower tower top pressure is controlled at absolute pressure 10～30kPa, 180～210 ℃ of tower top temperatures, 250～280 ℃ of carbolineum fraction extraction plate temperatures, cat head washing oil reflux ratio (to anhydrous tar) 0.1～0.3t/t.When producing viscid bitumen, 280～320 ℃ of column bottom temperatures, 310～350 ℃ of 2# tubular oven circulation pitch temperature outs.When producing mid-temperature pitch, 310～340 ℃ of anthracene oil fraction extraction plate temperatures, 340～370 ℃ of column bottom temperatures, 370～390 ℃ of 2# tubular oven circulation pitch temperature outs.
The 2# distillation tower is a tray column, can adopt the novel float valve in wide aperture, also can adopt the various new tower plate that are applicable to the coal tar medium, and material is a stainless steel, and 15～22 blocks of theoretical trays are arranged.
The structure of 2# tubular oven is identical with the 1# tubular oven, and material is a stainless steel.
Compare with existing tar distillation technology, the normal vacuum tar distil process of three-tower type of the present invention has the following advantages:
1. being separated under the normal pressure of dehydration of tar and light constituent carried out, and the separation of heavy constituent is under reduced pressure carried out, and temperature, pressure regime distribute rationally.Underpressure distillation not only reduced service temperature, reduced the gas consumption amount, but also improved operating environment, help environment protection;
2. cutting in two distillation towers of each fraction accomplished, and by the heat supply respectively of two tube furnaces, solved the technical barrier of handling extensive tar with single covering device;
3. technical process is short, control easy, easy handling, constant product quality, initial cost, equipment operation, maintenance cost are lower;
4. three distillation towers adopt the heat-supplying mode of oil circulation heating at the bottom of the tower, both have been convenient to operation and regulate, and can prevent the generation of coking again effectively;
5. fraction is cut apart carefullyyer, reduces the heating that repeats of following process fraction, reduces total energy consumption;
6. UTILIZATION OF VESIDUAL HEAT IN is abundant, and the heat of pitch and each fraction can be reclaimed and utilizes through heat exchange fully;
7. still-process need not feed open steam, does not produce to contain phenol, ammonia waste water;
8. tar preheating, dehydration etc. both can have been used steam heating, also can use heat-conducting oil heating, adapted to different engineering demands;
9. the fraction that be prone to crystallization, is prone to solidify cools off with warm water, minimizing equipment, line clogging,
10. can produce different asphaltic products.es, the demand of adaptation to market variations through the adjustment operating duty.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.Scheme coal-tar middle oil preheater, the dehydration tower reboiler is to be example with the heat-conducting oil heating.Asphaltic products. is to be example to produce mid-temperature pitch, when producing viscid bitumen, and the cancellation of 2# distillation tower anthracene oil side line.
Embodiment
Below in conjunction with accompanying drawing 1 and embodiment the present invention is done further explain.
As shown in Figure 1; After raw tar at first gets into tar/washing oil interchanger 18, tar/naphtalene oil interchanger 15, tar/carbolineum interchanger 20 and washing oil, naphtalene oil, a carbolineum fraction heat exchange; Advance tar preheater 9, by heat-conducting oil heating to 125～135 ℃, get into preparatory dehydration tower 1 then at this.
Dehydration tower is a flashing tower in advance; About 110～125 ℃ of tower top temperature; Light oil fraction that cat head is overflowed and water are cooled to 50～60 ℃ through 1# light oil air cooler 7 earlier, are cooled to 40～45 ℃ through 1# light oil water cooler 10 again, flow into 1# light oil water-and-oil separator 26; Isolated light oil as dehydration tower reflux with or time convert in the raw tar, flow into ammonia vessel after dividing dried up further separating oil.Tar at the bottom of the dehydration Tata is from flowing into dehydration tower 2 in advance.
Dehydration tower is operated under condition of normal pressure, and absolute pressure of top of the tower is 101～107kPa, and tower top temperature is 95～120 ℃; Distilled light oil fraction and water are cooled to 50～60 ℃ through 2# light oil air cooler 8 earlier; Be cooled to 40～45 ℃ through 2# light oil water cooler 11 again, flow into 2# light oil water-and-oil separator 27, isolate light oil at this; Part light oil send the dehydration cat head as backflow by dehydration tower reflux pump 29, and all the other send the oil depot device as product by light oil extraction pump 28; Flow into ammonia vessel after dividing dried up further separating oil, regularly by ammoniacal liquor transferpump gas delivery cleaning shop, isolated oil flows into the emptying groove.Dehydrated tar by dehydration tower at the bottom of extractor pump 31 extract out, send into the turning oil inlet tube of 1# tubular oven.
As thermal source, extract out with recycle pump at the bottom of the dehydration tower 30 by dehydration tower bed coke oil with thermal oil for dehydration tower, is heated to 195～230 ℃ through 12 circulations of dehydration tower reboiler, returns at the bottom of the dehydration tower to provide dehydration to distill institute's heat requirement.
1# distillation tower 3 is an atmospheric operation, and absolute pressure of top of the tower is 101～107kPa, and tower top temperature is 160～190 ℃, and from the condensation in 1# distillation tower reduction appts. 13 of cat head distilled carbolic oil vapour, a part is as refluxing from flowing back to cat head; Another part after carbolic oil water cooler 14 is cooled to 50～60 ℃, flows into the carbolic oil groove as the intermediates extraction, regularly delivers to the subsequent production device with the carbolic oil transferpump.
Cut the naphtalene oil fraction from 1# distillation tower 3 side lines; 210～240 ℃ of naphtalene oil fraction tower exit temperatures; Be introduced into tar/naphtalene oil interchanger 15 and give the tar preheating, extract out with naphtalene oil extraction pump 32 again, be cooled to 85～95 ℃ through naphtalene oil water cooler 16 usefulness warm water; Send the naphtalene oil groove to store, regularly deliver to the subsequent production device with the naphtalene oil transferpump.
1# distillation tower column bottom temperature is 265～295 ℃; A mixing oil part is extracted out with the next dehydrated tar of extractor pump at the bottom of the dehydration tower with 1# base product recycle pump 33 and is mixed at the bottom of the tower; Be heated to 290～320 ℃ through 1# tubular oven 5, get back to then at the bottom of the tower, distillation institute heat requirement is provided; Another part is extracted out by 1# base product extractor pump 34, sends into 2# tubular oven 6 circulation pitch inlet tubes.
1# distillation tower cat head non-condensable gases gets into exhaust system after 24 condensations of 1# distillation tower vent condenser.
The 2# distillation tower is a decompression operation, and absolute pressure of top of the tower is 10～30kPa, and tower top temperature is 180～210 ℃; Flow into cat head from the whole condensations in 2# distillation tower reduction appts. 17 of cat head distilled washing oil vapour, a part is as refluxing another part extraction; Be introduced into tar/washing oil interchanger 18 and give the tar preheating, extract out with washing oil extraction pump 35 again, be cooled to 70～80 ℃ through washing oil water cooler 19 usefulness warm water; Send oil groove to laundry and store, regularly deliver to the subsequent production device with the washing oil transferpump.
Cut a carbolineum fraction and anthracene oil fraction respectively from 2# distillation tower side line.250～280 ℃ of one carbolineum fraction tower exit temperatures; After tar/carbolineum interchanger 20 and tar heat exchange, extract out with a carbolineum extraction pump 36 again, be cooled to 85～95 ℃ through a carbolineum water cooler 21 usefulness warm water; Deliver to a carbolineum groove and store, a regular carbolineum transferpump is delivered to the subsequent production device.310～340 ℃ of anthracene oil fraction tower exit temperatures are cooled to 85～95 ℃ through anthracene oil water cooler 22 usefulness warm water, extract out with anthracene oil extraction pump 37 and deliver to the storage of anthracene oil groove, regularly deliver to the oil depot device with the anthracene oil transferpump.
2# distillation tower column bottom temperature is 340～370 ℃; A mid-temperature pitch part is extracted out with the next mixing oil of 1# base product extractor pump with 2# base product recycle pump 38 and is mixed at the bottom of the tower; Be heated to 370～390 ℃ through 2# tubular oven 6, get back to then at the bottom of the tower, distillation institute heat requirement is provided; Another part is extracted out after pitch/heat-condutive oil heat exchanger 23 and thermal oil heat exchange by 2# base product extractor pump 39, delivers to the subsequent production device.
When producing viscid bitumen at the bottom of the 2# distillation Tata, anthracene oil fraction extraction tube valve is closed, and this moment, 2# distillation tower column bottom temperature was 280～320 ℃, 310～350 ℃ of 2# tubular oven turning oil temperature outs.
The vacuum exhaust of 2# distillation tower is through the laggard vacuum system of 2# distillation tower vacuum exhaust condensing surface 25 condensations,
Described dehydration tower, 1# distillation tower and 2# distillation tower are tray column.Dehydration tower has 6～10 blocks of theoretical trays, and the 1# distillation tower has 22～32 blocks of theoretical trays, and the 2# distillation tower has 15～22 blocks of theoretical trays, all adopts the novel float valve in wide aperture or is applicable to the various new tower plate of coal tar medium.The dehydration tower material is a carbon steel, and 1# distillation tower and 2# distillation tower material are stainless steel.
Described dehydration tower reboiler is vertical liquid film downward flow type structure.
Described 1# tubular oven and 2# tubular oven are vertical coil pipe cylindrical furnace, and furnace tube material is a stainless steel.
Described interchanger, water cooler are shell-and-tube, according to different choice stationary tubesheet, U type pipe or the floating head type of fluid properties.The interchanger material is selected carbon steel or stainless steel for use according to the corrosion situation of medium.
Claims (5)
1. the normal vacuum tar distil process of three-tower type is characterized in that, may further comprise the steps:
1) raw tar is removing moisture and extraction light oil fraction in dehydration tower, the dehydration tower in advance under condition of normal pressure, and the heat of dehydration tower, dehydration tower is provided by thermal oil or steam in advance;
2) dehydrated tar under condition of normal pressure in the 1# distillation tower fractionation by distillation, cat head extraction carbolic oil fraction, side line cuts the naphtalene oil fraction; The heat of 1# distillation tower by tower at the bottom of mixing oil provide in 1# tubular oven internal recycle heating;
3) 1# base product mixing oil in the 2# distillation tower under reduced pressure fractionation by distillation obtain washing oil, a carbolineum, anthracene oil fraction and asphaltic products.; Or washing oil, a carbolineum fraction and viscid bitumen product, the heat of 2# distillation tower by tower at the bottom of pitch provide in 2# tubular oven internal recycle heating.
2. the normal vacuum tar distil process of three-tower type according to claim 1; It is characterized in that; After described raw tar at first gets into tar/washing oil interchanger, tar/naphtalene oil interchanger, tar/carbolineum interchanger and washing oil, naphtalene oil, a carbolineum fraction heat exchange; Get into the tar preheater, get into preparatory dehydration tower then.
3. the normal vacuum tar distil process of three-tower type according to claim 1 and 2; It is characterized in that; Described dehydration column overhead pressure-controlling is at absolute pressure 101～107kPa, 95～120 ℃ of tower top temperatures, 180～210 ℃ of column bottom temperatures; 195～230 ℃ of dehydration tower reboiler circulation tar temperature outs, dehydration column overhead light oil is to anhydrous tar reflux ratio 0.02～0.04t/t.
4. the normal vacuum tar distil process of three-tower type according to claim 1 and 2; It is characterized in that described 1# distillation tower tower top pressure is controlled at absolute pressure 101～107kPa, 160～190 ℃ of tower top temperatures; 210～240 ℃ of naphtalene oil fraction extraction plate temperatures; 265～295 ℃ of column bottom temperatures, 290～320 ℃ of 1# tubular oven turning oil temperature outs, the cat head carbolic oil is to anhydrous tar reflux ratio 0.45～0.7t/t.
5. the normal vacuum tar distil process of three-tower type according to claim 1 and 2; It is characterized in that; Described 2# distillation tower tower top pressure is controlled at absolute pressure 10～30kPa; 180～210 ℃ of tower top temperatures, 250～280 ℃ of carbolineum fraction extraction plate temperatures, the cat head washing oil is to anhydrous tar reflux ratio 0.1～0.3t/t; When producing viscid bitumen, 280～320 ℃ of column bottom temperatures, 310～350 ℃ of 2# tubular oven circulation pitch temperature outs; When producing mid-temperature pitch, 310～340 ℃ of anthracene oil fraction extraction plate temperatures, 340～370 ℃ of column bottom temperatures, 370～390 ℃ of 2# tubular oven circulation pitch temperature outs.
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| CN110016358A (en) * | 2019-03-18 | 2019-07-16 | 中国铝业股份有限公司 | A kind of processing and application method of aluminium cathode charcoal roasting gas cleaning tar |
| CN110484289A (en) * | 2019-09-24 | 2019-11-22 | 济宁黑猫炭黑有限责任公司 | A kind of tar negative pressure dewatering system and method |
| CN113150811A (en) * | 2020-01-07 | 2021-07-23 | 上海圣升化工科技有限公司 | Coal tar deep processing technology |
| CN115433602A (en) * | 2022-08-31 | 2022-12-06 | 宝钢工程技术集团有限公司 | Dehydration tower series heating device for tar processing and use method thereof |
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